CN112142246A - High-salt high-organic-matter wastewater zero-discharge treatment process - Google Patents
High-salt high-organic-matter wastewater zero-discharge treatment process Download PDFInfo
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- 239000002351 wastewater Substances 0.000 title claims abstract description 91
- 238000000034 method Methods 0.000 title claims abstract description 49
- 208000028659 discharge Diseases 0.000 title claims abstract description 42
- 239000005416 organic matter Substances 0.000 title claims description 17
- 238000000926 separation method Methods 0.000 claims abstract description 136
- 239000007788 liquid Substances 0.000 claims abstract description 86
- 150000003839 salts Chemical class 0.000 claims abstract description 83
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 65
- 239000012452 mother liquor Substances 0.000 claims abstract description 36
- 238000009833 condensation Methods 0.000 claims abstract description 23
- 230000005494 condensation Effects 0.000 claims abstract description 23
- 230000000694 effects Effects 0.000 claims description 171
- 238000004064 recycling Methods 0.000 claims description 23
- 239000011259 mixed solution Substances 0.000 claims description 18
- 239000013078 crystal Substances 0.000 claims description 12
- 238000005086 pumping Methods 0.000 claims description 12
- 238000003860 storage Methods 0.000 claims description 12
- 238000002156 mixing Methods 0.000 claims description 9
- 239000000243 solution Substances 0.000 claims description 8
- 230000009291 secondary effect Effects 0.000 claims description 7
- 239000012266 salt solution Substances 0.000 claims description 4
- 239000007787 solid Substances 0.000 claims description 3
- 238000001704 evaporation Methods 0.000 abstract description 66
- 230000008020 evaporation Effects 0.000 abstract description 66
- 238000002425 crystallisation Methods 0.000 abstract description 9
- 230000008025 crystallization Effects 0.000 abstract description 9
- 238000012546 transfer Methods 0.000 abstract description 9
- 238000010438 heat treatment Methods 0.000 abstract description 5
- 239000007789 gas Substances 0.000 description 40
- 238000001035 drying Methods 0.000 description 4
- 238000012423 maintenance Methods 0.000 description 4
- 238000004806 packaging method and process Methods 0.000 description 4
- 238000005192 partition Methods 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- 230000009286 beneficial effect Effects 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 239000012528 membrane Substances 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012856 packing Methods 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 239000013589 supplement Substances 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- 238000004065 wastewater treatment Methods 0.000 description 2
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 238000004891 communication Methods 0.000 description 1
- 239000000498 cooling water Substances 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000011010 flushing procedure Methods 0.000 description 1
- 238000002955 isolation Methods 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 238000001223 reverse osmosis Methods 0.000 description 1
- 238000009287 sand filtration Methods 0.000 description 1
- 239000002893 slag Substances 0.000 description 1
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- 239000002562 thickening agent Substances 0.000 description 1
- 238000000108 ultra-filtration Methods 0.000 description 1
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/048—Purification of waste water by evaporation
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F2001/5218—Crystallization
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/30—Organic compounds
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2301/00—General aspects of water treatment
- C02F2301/08—Multistage treatments, e.g. repetition of the same process step under different conditions
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Abstract
The invention discloses a high-salt high-organic wastewater zero-discharge treatment process, which comprises the steps of preheating high-salt high-organic wastewater, then heating the high-salt high-organic wastewater in a multi-effect evaporation separation unit, carrying out vapor-liquid separation on the high-salt high-organic wastewater, enabling the concentrated wastewater generated by the vapor-liquid separation of the multi-effect evaporation separation unit to enter a crystallized salt separation unit to realize solid-liquid separation to form crystallized salt and mother liquor, enabling the mother liquor to enter a mixed salt separation unit to carry out evaporation crystallization and solid-liquid separation to form mixed salt and steam, enabling secondary steam generated by the vapor-liquid separation of the multi-effect evaporation separation unit to enter a condensation unit to be condensed to form condensed water, enabling the secondary steam generated by the vapor-liquid separation of the mixed salt separation unit to enter the condensation, the non-condensable gas in the condensing unit can be discharged out of the process system in time by vacuumizing, so that the heat transfer efficiency of the system is greatly improved.
Description
Technical Field
The invention relates to the technical field of wastewater treatment, in particular to a high-salinity high-organic-matter wastewater zero-discharge treatment process.
Background
At present, the treatment process of industrial salt and organic matter containing wastewater mainly comprises a series of pretreatment and concentration process units such as pretreatment, biochemical treatment, high-efficiency oxidation, sand filtration, ultrafiltration, reverse osmosis and the like, and the high-salt and high-organic matter (TDS is more than or equal to 50000mg/L, COD is more than or equal to 500mg/L) wastewater generated by the system is mainly used for dedusting and slag flushing of coal yards or indirect discharge. With the increasingly strengthened zero discharge of wastewater from enterprises required by national environmental protection policies, the zero discharge treatment of high-salt and high-organic wastewater generated by the membrane concentration process is one of the important directions for environmental protection treatment of enterprises.
The current zero-emission treatment process of high-salinity high-organic-matter wastewater generated by a membrane concentration process mainly comprises evaporative crystallization, and the process has the advantages of simple flow, convenience in operation, small occupied area and the like, and is popular with various large enterprises. However, the existing evaporative crystallization process is mainly a multi-effect evaporative crystallization process or an MVR evaporative crystallization process, but has the disadvantages of poor operation stability, easy blockage of a heating pipe, weak evaporation treatment capacity, high equipment investment and high operation and maintenance cost, and particularly, the MVR vapor compressor has frequent failure, the equipment replacement and maintenance period is long, and great confusion is brought to the normal production of enterprises.
Disclosure of Invention
The invention mainly aims to provide a high-salinity high-organic wastewater zero-discharge treatment process, and aims to provide a high-salinity high-organic wastewater treatment process with good stability, less discharge and even zero discharge.
In order to realize the aim, the invention provides a high-salinity high-organic-matter wastewater zero-discharge treatment process, which comprises the following steps of:
step S210: preheating high-salt high-organic wastewater by a first steam condenser and a preheater in sequence, enabling a first mixed solution formed by mixing the preheated high-salt high-organic wastewater with a circulating liquid of a first effect heater to enter the first effect heater, performing heat exchange with raw steam in the first effect heater to reach a preset temperature, condensing the raw steam to generate condensed water for recycling, and performing steam-liquid separation on the first mixed solution at the preset temperature in a first effect separator to generate secondary steam;
step S220: the secondary steam generated by the first effect separator enters a second effect heater, the wastewater evaporated and concentrated by the first effect separator enters the second effect heater, a second mixed solution formed by mixing the wastewater with a circulating liquid of the second effect heater is heated to a preset temperature by the secondary steam generated by the first effect separator, the secondary steam after heat exchange is condensed to generate condensed water for recycling, and the second mixed solution at the preset temperature is subjected to vapor-liquid separation in the second effect separator to generate secondary steam again;
step S230: the secondary steam generated by the second effect separator enters a third effect heater, the wastewater evaporated and concentrated by the second effect separator enters the third effect heater, a third mixed solution formed by mixing the wastewater with the circulating liquid of the third effect heater is heated to a preset temperature by the secondary steam generated by the second effect separator, the secondary steam after heat exchange is condensed to generate condensed water for recycling, and the third mixed solution at the preset temperature is subjected to vapor-liquid separation in the third effect separator to generate secondary steam again;
step S240: the secondary steam generated by the third effect separator enters the first steam condenser for condensation to form steam condensate water for recycling, the waste water evaporated and concentrated by the third effect separator generates crystallized salt in the third effect separator, a part of crystallized salt solution is subjected to solid-liquid separation by a crystallized salt separation device, the separated crystallized salt is dried and stored, a part of separated crystallized salt mother liquor returns to the third effect separator, the other part of separated crystallized salt mother liquor enters an externally-discharged mother liquor evaporator, the generated secondary steam enters the second steam condenser for condensation to form steam condensate water for recycling, the produced miscellaneous salt crystal solution passes through the externally-discharged mother liquor evaporator and is subjected to solid-liquid separation, miscellaneous salt solids obtained by solid-liquid separation are stored, and the miscellaneous salt mother liquor returns to a mother liquor storage tank.
Preferably, the method further comprises the following steps:
step S250: the non-condensable gas in the first effect heater, the second effect heater and the third effect heater enters a vacuum device for vacuum pumping.
Preferably, the method further comprises the following steps:
step S260: and non-condensable gas in the first steam condenser and the second steam condenser enters a vacuum device for vacuum pumping.
Preferably, the step of recycling condensed water generated by condensing the secondary steam after heat exchange in step S220 specifically includes:
and the secondary steam after heat exchange is condensed and enters a secondary steam condensation water tank through a secondary effect buffer tank.
Preferably, the noncondensable gas in the second effect buffer tank and the secondary steam condensate water tank enters a vacuum device for vacuumizing.
Preferably, the step of recycling condensed water generated by condensing the secondary steam after heat exchange in step S230 specifically includes:
and the secondary steam after heat exchange is condensed and enters a secondary steam condensate water tank through a third effect buffer tank.
Preferably, the noncondensable gas in the third effect buffer tank and the secondary steam condensate water tank enters a vacuum device for vacuumizing.
Preferably, the circulating liquid between the first effect heater and the first effect separator is operated in a forced circulation mode; and/or the presence of a gas in the gas,
circulating liquid between the second-effect heater and the second-effect separator operates in a forced circulation mode; and/or the presence of a gas in the gas,
and circulating liquid between the third-effect heater and the third-effect separator operates in a forced circulation mode.
Preferably, a first effect circulating pump is connected between the first effect heater and the first effect separator; a second-effect circulating pump is connected between the second-effect heater and the second-effect separator; and a third-effect circulating pump is connected between the third-effect heater and the third-effect separator.
Preferably, the first effect heater, the second effect heater, and the third effect heater are of the same type; and/or the first effect separator, the second effect separator, and the third effect separator are of the same type.
The invention has the following beneficial effects:
(1) zero waste liquid discharge of the high-salinity high-organic wastewater is realized (the generated condensed water can be directly utilized without other water generation).
(2) The condensed water generated by condensing the generated steam and the secondary steam in the process can be used as water for the production process or water supplement of a circulating cooling system, and the recovery rate of the produced water is close to 100 percent.
(3) The process flow is simple and convenient to operate.
Drawings
One or more embodiments are illustrated by way of example in the accompanying drawings, which correspond to the figures in which like reference numerals refer to similar elements and which are not to scale unless otherwise specified.
FIG. 1 is a block diagram of a high-salinity high-organic wastewater zero-discharge treatment system according to an embodiment of the present invention;
fig. 2 is a flow chart of an embodiment of the high-salinity high-organic wastewater zero-discharge treatment process provided by the invention.
The invention is illustrated by the reference numerals:
the implementation, functional features and advantages of the objects of the present invention will be further explained with reference to the accompanying drawings.
Detailed Description
In order to make the objects, technical solutions and advantages of the embodiments of the present invention clearer, the technical solutions in the embodiments of the present invention will be clearly and completely described below. The examples, in which specific conditions are not specified, were conducted under conventional conditions or conditions recommended by the manufacturer. The reagents or instruments used are not indicated by the manufacturer, and are all conventional products available commercially.
The invention provides a high-salinity high-organic wastewater zero-discharge treatment system, referring to fig. 1, the high-salinity high-organic wastewater zero-discharge treatment system comprises a multi-effect evaporation separation unit 1, a condensation unit 2, a vacuum device 3, a crystallized salt separation unit 4 and a miscellaneous salt separation unit 5, wherein a steam pipeline 71, a concentrated wastewater pipeline 73 and a noncondensable gas pipeline 72 of two adjacent effect evaporation separation units 1 are respectively and sequentially communicated, a shell pass of the condensation unit 2 is communicated with the steam pipeline 71 and the noncondensable gas pipeline 72 of the last effect evaporation separation unit 1, the vacuum device 3 is communicated with a shell pass of the condensation unit 2 and is used for vacuumizing noncondensable gas, the crystallized salt separation unit 4 is communicated with the concentrated wastewater pipeline 73 of the last effect evaporation separation unit 1 and is used for realizing the separation of concentrated wastewater, a liquid inlet of the miscellaneous salt separation unit 5 is communicated with a liquid outlet of the crystallized salt separation unit 4, and a steam outlet is communicated with the shell side of the condensing unit 2 so as to carry out solid-liquid separation on the mother liquor discharged from the crystallized salt separation unit 4.
The invention preheats high-salt high-organic wastewater, then enters a multi-effect evaporation separation unit 1 for heating and vapor-liquid separation, the concentrated wastewater generated by the vapor-liquid separation of the multi-effect evaporation separation unit 1 enters a crystal salt separation unit 4 for realizing solid-liquid separation to form crystal salt and mother liquor, the mother liquor enters a miscellaneous salt separation unit 5 for evaporation crystallization and solid-liquid separation to form miscellaneous salt and steam, the secondary steam generated by the vapor-liquid separation of the multi-effect evaporation separation unit 1 enters a condensation unit for condensation to form condensed water, the secondary steam generated by the vapor-liquid separation of the miscellaneous salt separation unit 5 enters the condensation unit for condensation to form condensed water, the non-condensable gas in the multi-effect evaporation separation unit 1 and the condensation unit 2 is pumped by a vacuum device to discharge the non-condensable gas in a process system in time, the heat transfer efficiency of the system is greatly improved, and the evaporation treatment capacity of the process system is further improved, the stability of the system is improved, the high-salinity and high-organic-matter wastewater is converted into condensate water for recycling, salt in the wastewater is converted into crystal salt and miscellaneous salt for storage, the zero discharge of the high-salinity and high-organic-matter wastewater is realized, meanwhile, equipment in the system is very mature equipment for industrial use, and the maintenance cost is low.
In the present embodiment, the condensing unit 2 includes a first steam condenser 21 and a second steam condenser 22, a shell side of the first steam condenser 21 is communicated with the steam pipeline 71 and the non-condensable gas pipeline 72 of the last-effect evaporation and separation unit 1, and a shell side of the second steam condenser 22 is communicated with the steam outlet of the mixed salt separation unit 5; the vacuum device 3 is connected to a pipeline communicated with the shell side of the first steam condenser 21 and the shell side of the second steam condenser 22. The shell pass of the first steam condenser 21 and the steam pipeline 71 of the last-effect evaporation and separation unit 1 can condense the secondary steam generated by the multi-effect evaporation and separation unit 1 into condensed water; the shell pass of first steam condenser 21 communicates with noncondensable gas pipeline 72, and vacuum device 3 is connected the pipeline of the shell pass of first steam condenser 21, the shell pass intercommunication of second steam condenser 22, so can be to noncondensable gas pipeline 72, the shell pass of first steam condenser 21, the noncondensable gas in the shell pass of second steam condenser 22 carry out the evacuation, can in time discharge noncondensable gas in the process system, improved system heat transfer efficiency greatly, and then improved process system's evaporation treatment ability.
The mixed salt separation unit 5 may be a conventional mixed salt separation unit 5, in this embodiment, the mixed salt separation unit 5 includes an external discharge mother liquor evaporator 51 and a mixed salt separation device 52, the external discharge mother liquor evaporator 51 is communicated with a liquid discharge port of the crystallized salt separation unit 4, a steam pipeline 71 of the external discharge mother liquor evaporator 51 is communicated with a shell pass of the second steam condenser 22, and the mixed salt separation device 52 is connected with a wastewater pipeline of the external discharge mother liquor evaporator 51. The mother liquor is separated from vapor and liquid by an externally discharged mother liquor evaporator 51, the separated secondary vapor enters the shell side of the second vapor condenser 22 for condensation, and the concentrated liquid forms a crystallized salt solution which is subjected to solid-liquid separation by a mixed salt separation device 52 to form mixed salt. In other embodiments, the mixed salt separation unit 5 further includes a mother liquor storage tank 53, the mother liquor storage tank 53 is respectively communicated with the crystallized salt separation unit 4, the discharged mother liquor evaporator 51, the mixed salt separation device 52, and the concentrated waste water pipeline 73 of the last effect evaporation separation unit 1, so that the mother liquor enters the discharged mother liquor evaporator 51 through the mother liquor storage tank 53, and the liquid remaining after the separation of the mixed salt separation device 52 can be returned to the mother liquor storage tank 53 for recycling treatment. The mixed salt separating unit 5 can also comprise a mixed salt packing machine 54 connected with the mixed salt separating device 52, and a mixed salt outgoing storage 55 connected with the mixed salt packing machine 54, so as to pack and transport the mixed salt for storage.
The crystallized salt separation unit 4 comprises a crystallized salt separation device 41 (in this embodiment, the crystallized salt separation device 41 may comprise a thickener or a cyclone, a buffer tank, a solid-liquid separation device, and the like, and the solid-liquid separation device may be a centrifuge or a plate-and-frame filter press or other devices capable of realizing solid-liquid separation), a drying device 42, and a crystallized salt packaging machine 43, wherein a liquid inlet of the crystallized salt separation device 41 is communicated with the concentrated waste water pipeline 73 of the final effect evaporation separation unit 1, a liquid outlet of the crystallized salt separation device is communicated with a liquid inlet of the mixed salt separation unit 5, and the drying device 42 is connected with the crystallized salt separation device 41 and is used for drying crystallized salt after crystallization; and a crystallized salt packaging machine 43 connected to the drying device 42 for packaging the dried crystallized salt. In other embodiments, the crystallized salt isolation unit 4 may also include a crystallized salt outgoing storage 44 connected to the crystallized salt packaging machine 43 so that the crystallized salt may be transported for storage.
Each effect of the evaporation separation unit 1 comprises a separator, a heater and a circulating pump, wherein two ends of a tube pass of the heater are respectively communicated with a liquid inlet and a liquid outlet of the separator, and the circulating pump is arranged on a pipeline for communicating the liquid outlet of the separator with the tube pass of the heater; the liquid outlet of the separator of evaporation and separation unit 1, respectively with adjacent next effect evaporation and separation unit 1's the liquid outlet of separator with the circulating pump intercommunication, so, through last effect evaporation and separation unit 1 (use first effect as the example) the separator steam separation concentrated waste water through next effect evaporation and separation unit 1 (last effect is when first effect, here next effect is second effect) the circulating pump get into the tube side heating of next effect evaporation and separation unit 1's heater, reentrant separator separation, the steam that the separation formed gets into the shell side of next effect evaporation and separation unit 1 (last effect is when first effect, here next effect is the third effect)'s heater, … …. Because every effect evaporation and separation unit 1 the circulating pump sets up the liquid outlet of separator with on the pipeline of the tube side intercommunication of heater, the concentrated waste water after every effect evaporation and separation unit 1's separator separation concentration can get into the tube side of the corresponding heater through the liquid outlet of separator, circulating pump, so carry out the circulation and handle.
Raw steam circulates on the shell side of a heater of the first-effect evaporation separation unit 1, so that the raw steam and the wastewater exchange heat to heat the wastewater; the high-salinity high-organic-matter wastewater zero-emission treatment system further comprises a preheater 114, wherein the preheater 114 is communicated with a tube pass of a heater of the first-effect evaporation separation unit 1. In this way, the wastewater enters the tube pass of the heater of the first-effect evaporation separation unit 1 through the preheater 114 and the circulating pump of the first-effect evaporation separation unit 1, and the wastewater and the raw steam fully exchange heat in a partition wall heat transfer mode to heat the wastewater.
The preheater 114 is respectively communicated with the shell pass of the heater of the first-effect evaporation separation unit 1 and the raw steam condensate water tank 61, and is used for enabling condensate water generated by condensation of the raw steam after heat exchange with the wastewater to enter the raw steam condensate water tank 61 through the preheater 114.
The shell pass of the heater of the evaporation separation unit 1 with secondary effect (secondary effect and above) is sequentially communicated with a buffer tank and a secondary steam condensate tank, and condensate water generated by condensing secondary steam enters the secondary steam condensate tank through the buffer tank; the buffer tank of the secondary effect evaporation separation unit 1 is communicated with the shell pass of the heater of the next effect evaporation separation unit 1, so that the non-condensable gas in the buffer tank can be vacuumized by the vacuum device 3 through the shell pass of the heater of the next effect evaporation separation unit 1; and the buffer tank of the final-effect evaporation separation unit 1 is communicated with the shell pass of the condensation unit 2. Preferably, the secondary steam condensate tank is in communication with the shell side of the first steam condenser 21 for collecting condensate in the first steam condenser 21.
The shell sides of the heaters of the two adjacent effect evaporation separation units 1 are communicated to form the non-condensable gas pipeline 72. The shell pass of the first steam condenser 21 is communicated with the non-condensable gas pipeline 72, so that non-condensable gas in the process system can be discharged in time, the heat transfer efficiency of the system is greatly improved, and the evaporation treatment capacity of the process system is further improved.
The multi-effect evaporation and separation unit 1 can be a three-effect or four-effect unit … … in the embodiment, the multi-effect evaporation and separation unit 1 is a three-effect evaporation and separation unit, and each effect of the evaporation and separation unit has the same structure. The triple-effect evaporation and separation units are respectively a first evaporation and separation unit 11, a second evaporation and separation unit 12 and a third evaporation and separation unit 13, wherein the heater in the first evaporation and separation unit is a first-effect heater 111, the separator in the first evaporation and separation unit is a first-effect separator 112, and the circulating pump in the first evaporation and separation unit is a first-effect circulating pump 113; the heater in the second evaporation and separation unit 12 is a second-effect heater 121, the separator in the second evaporation and separation unit 12 is a second-effect separator 122, the circulating pump in the second evaporation and separation unit 12 is a second-effect circulating pump 123, and the corresponding buffer tank is a second-effect buffer tank 124; the heater in the third evaporation and separation unit 13 is a third-effect heater 131, the separator in the third evaporation and separation unit 13 is a third-effect separator 132, the circulating pump in the third evaporation and separation unit 13 is a third-effect circulating pump 133, and the corresponding buffer tank is a third-effect buffer tank 134.
Specifically, the tube pass of the first steam condenser 21 is divided into a cold source tube pass 211 and a material water tube pass 212, the material water tube pass 212 is communicated with the preheater 114, and the high-salt and high-organic wastewater can enter the tube pass of the first effective heater 111 which passes through the preheater 114 and the first circulating pump from the material water tube pass 212, so that the high-salt and high-organic wastewater can be preheated in the first steam condenser 21 and the preheater 114. The cold source pipeline is connected with the cold source (cooling water in the embodiment).
A first evaporative separation unit: the circulating liquid of the first effect heater 111 and the high-salt and high-organic wastewater preheated by the first steam condenser 21 and the preheater 114 are mixed and enter a tube pass of the first effect heater 111, heat is fully exchanged with raw steam in a partition wall heat transfer mode, condensed water generated by condensation of the raw steam enters the raw steam condensate water tank 61 after passing through the preheater 114, the heated circulating liquid and the high-salt and high-organic wastewater enter the first effect separator 112 for steam-liquid separation, the generated secondary steam enters a shell pass of the second effect heater 121 (in the embodiment, the secondary steam enters the second effect heater 121 after being demisted by a demister first), and the evaporated and concentrated wastewater can be returned to the first effect heater 121 for continuous circulating treatment or can enter the second effect heater 121;
the second evaporative separation unit 12: the circulating liquid of the second-effect heater 121 and the wastewater after the first-effect evaporation and concentration are mixed and enter a tube pass of the second-effect heater 121, then the heat is fully exchanged with the secondary steam from the first-effect separator 112 through a partition wall heat transfer mode, the condensed water generated by condensation of the secondary steam after the heat exchange enters the secondary steam condensate water tank 62 after passing through the second-effect buffer tank 124, the heated circulating liquid and the concentrated wastewater enter the second-effect separator 122 for steam-liquid separation, the generated secondary steam enters the third-effect heater 131 after being demisted by a demister, and the wastewater after the evaporation and concentration can be returned to the second-effect heater 121 for continuous circulating treatment or can enter the third-effect heater 131;
the third evaporation separation unit 13: the third effect heater 131 mixes the circulating liquid with the waste water after the second effect evaporation concentration and enters the third effect heater 131, then secondary steam discharged from the second effect separator 122 fully exchanges heat through a partition wall heat transfer mode, condensed water generated by condensation of the secondary steam after heat exchange enters the secondary steam condensate water tank 62 after passing through the third effect buffer tank 134, the heated circulating liquid and the concentrated waste water enter the third effect separator 132 for steam-liquid separation, the generated secondary steam enters the first steam condenser 21 after demisting through a demister, and the condensed water generated by condensation enters the secondary steam condensate water tank 62. The waste water after evaporation concentration generates crystal salt in the third effect separator 132, most of the crystal salt circulating liquid formed by the crystal salt and the circulating liquid returns to the third effect heater 131, and a certain amount of the crystal salt circulating liquid enters the crystal salt separation device 41 for solid-liquid separation.
In the present embodiment, the first effect heater 111, the second effect heater 121 and the third effect heater 131 are all the same type of heater, and the first effect separator 112, the second effect separator 122 and the third effect separator 132 are all the same type of vapor-liquid separator.
The circulating liquid between the n-th effect heater and the n-th effect separator (n is 1, 2, 3 and 4 …) adopts a forced circulation operation mode;
the top of the n-th efficient separator (n is 1, 2, 3 and 4 …) is provided with a demister and a cleaning spray head;
the main function of the vacuum device 3 is to pump out the non-condensable gas in the system, and mainly comprises:
(1) non-condensable gasses in the first effect heater 111, the second effect heater 121, and the third effect heater 131;
(2) noncondensable gas in the second effect buffer tank 124, the third effect buffer tank 134 and the secondary steam condensate water tank 62;
(3) non-condensable gases in the first and second steam condensers 21 and 22;
the non-condensable gas pipelines 72 of the 3 devices are communicated to form a non-condensable gas pipeline 72 system, and the non-condensable gas in the system is vacuumized by the vacuum device 3. The method specifically comprises the following steps: the non-condensable gas pipelines 72 of the first effect heater 111, the second effect heater 121 and the third effect heater 131 are communicated with the steam pipeline 71 of the third effect separator 132, and the steam pipeline 71 of the third effect separator 132 is communicated with the steam condenser 1; the non-condensable gas pipeline 72 of the second-effect buffer tank 124 is communicated with the steam pipeline 71 of the second-effect separator 122, and the steam pipeline 71 of the second-effect separator 122 is communicated with the third-effect heater 131; the non-condensable gas pipeline 72 of the third-effect buffer tank 134 and the non-condensable gas pipeline 72 of the secondary steam condensate water tank 62 are communicated with the steam condenser 1; the non-condensable gas pipelines of the steam condenser 1 and the steam condenser 2 are communicated with a vacuum device, so that the vacuum device 3 can complete the vacuum pumping of the non-condensable gas in the system.
The invention has the following beneficial effects:
(1) zero waste liquid discharge of the high-salinity high-organic wastewater is realized (the generated condensed water can be directly utilized without other water generation).
(2) The condensed water generated by condensing the generated steam and the secondary steam in the system can be used as water for the production process or water supplement of a circulating cooling system, and the recovery rate of the produced water is close to 100 percent.
(3) The whole system flow is simple and convenient to operate.
(4) The whole system adopts a downstream feeding mode, a noncondensable gas process pipeline and a condensing mode of secondary steam in the first steam condenser 21 are reasonably designed, the evaporation treatment capacity of the process system is improved, and the system has the characteristics of high operation stability, difficulty in blockage of a heating pipe, low equipment investment, low operation and maintenance cost and the like.
The invention also provides a high-salinity high-organic matter wastewater zero-discharge treatment process, referring to fig. 2, which comprises the following steps:
step S210: preheating high-salt high-organic wastewater by a first steam condenser 21 and a preheater 114 in sequence, feeding a first mixed solution formed by mixing the preheated high-salt high-organic wastewater with a circulating liquid of a first effect heater 111 into a tube pass of the first effect heater 111, performing heat exchange with raw steam in the first effect heater 111 to reach a preset temperature, condensing the raw steam to generate condensed water for recycling, and performing steam-liquid separation on the first mixed solution at the preset temperature in a first effect separator 112 to generate secondary steam;
specifically, the circulating liquid between the first effect heater 111 and the first effect separator 112 is operated in a forced circulation manner, in this embodiment, the first effect circulating pump 113 is connected between the first effect heater 111 and the first effect separator 112, so that the first effect heater 111 can be heated effectively by preventing the solution from being blocked by crystals.
Step S220: the secondary steam generated by the first effect separator 112 enters the second effect heater 121, the wastewater evaporated and concentrated by the first effect separator 112 enters the second effect heater 121, a second mixed solution formed by mixing the wastewater with the circulating liquid of the second effect heater 121 is heated to a preset temperature by the secondary steam generated by the first effect separator 112, the secondary steam after heat exchange is condensed to generate condensed water for recycling, and the second mixed solution at the preset temperature is subjected to vapor-liquid separation in the second effect separator 122 to generate secondary steam again;
specifically, the step of recycling condensed water generated by condensing the secondary steam after the heat exchange in step S220 specifically includes:
the secondary steam after heat exchange is condensed and enters the secondary steam condensate water tank 62 through the secondary effect buffer tank 124.
Further, the circulating liquid between the second-effect heater 121 and the second-effect separator 122 is operated in a forced circulation manner, in this embodiment, a second-effect circulating pump 123 is connected between the second-effect heater 121 and the second-effect separator 122, so that the second-effect heater 121 can be effectively heated by preventing the solution from being blocked by crystallization.
Step S230: the secondary steam generated by the second effect separator 122 enters the third effect heater 131, the wastewater evaporated and concentrated by the second effect separator 122 enters the third effect heater 131, and a third mixed solution formed by mixing the wastewater with the circulating liquid of the third effect heater 131 is heated to a preset temperature by the secondary steam generated by the second effect separator 122, the secondary steam after heat exchange is condensed to generate condensed water for recycling, and the vapor-liquid separation of the third mixed solution at the preset temperature in the third effect separator 132 generates secondary steam again;
specifically, the circulating liquid between the third-effect heater 131 and the third-effect separator 132 is operated in a forced circulation manner, and in this embodiment, the third-effect circulating pump 133 is connected between the third-effect heater 131 and the third-effect separator 132, so that the third-effect heater 131 can be effectively heated by preventing the solution from being blocked by crystallization.
Step S240: the secondary steam generated by the third effect separator 132 enters the first steam condenser 21 to be condensed to form steam condensate water for recycling, the wastewater evaporated and concentrated by the third effect separator 132 generates crystallized salt in the third effect separator 132, a part of crystallized salt solution is subjected to solid-liquid separation by the crystallized salt separation device 41, the separated crystallized salt is dried and stored, a part of separated crystallized salt mother liquor returns to the third effect separator 132, the other part of separated crystallized salt mother liquor enters the discharged mother liquor evaporator 51, the generated secondary steam enters the second steam condenser 22 to be condensed to form steam condensate water for recycling, the mixed salt crystal solution generated by the discharged mother liquor evaporator 51 is subjected to solid-liquid separation, the mixed salt solid obtained by solid-liquid separation is stored, and the mixed salt mother liquor returns to the mother liquor storage tank 53.
Preferably, the method further comprises the following steps:
step S250: the non-condensable gas in the first effect heater 111, the second effect heater 121 and the third effect heater 131 enters the vacuum device 3 for vacuum pumping.
Preferably, the method further comprises the following steps:
step S260: the non-condensable gas in the first steam condenser 21 and the second steam condenser 22 enters the vacuum device 3 for vacuum pumping.
Preferably, the noncondensable gas in the second effect buffer tank 124 and the secondary steam condensate water tank 62 enters the vacuum device 3 for vacuum pumping.
Preferably, the step of recycling condensed water generated by condensing the secondary steam after heat exchange in step S230 specifically includes:
the secondary steam after heat exchange is condensed and enters a secondary steam condensate water tank 62 through a third effect buffer tank 134.
Preferably, the noncondensable gas in the third effect buffer tank 134 and the secondary steam condensate water tank 62 enters the vacuum device 3 for vacuum pumping.
Noncondensable gas in the system can be discharged in time through the vacuum pumping of the vacuum device 3, the heat transfer efficiency of the system is greatly improved, and the evaporation treatment capacity is further improved.
The first effect heater 111, the second effect heater 121, and the third effect heater 131 are of the same type; the first effect separator 112, the second effect separator 122 and the third effect separator 132 are of the same type.
It should be noted that, steps S210 to S260 may not be in sequence, may be in parallel, or may be in a sequential relationship, and are not limited specifically herein.
It should be noted that the embodiment of the high-salinity high-organic wastewater zero-discharge treatment system provided by the present invention is an embodiment of a device corresponding to a high-salinity high-organic wastewater zero-discharge treatment process, and therefore, the embodiment of the device provided by the present invention can be implemented in cooperation with the process embodiment. The relevant technical details mentioned in the embodiment of the high-salt high-organic wastewater zero-discharge treatment system are still effective in the high-salt high-organic wastewater zero-discharge treatment process, and the technical effects that can be achieved in the embodiment of the high-salt high-organic wastewater zero-discharge treatment system can also be achieved in the embodiment of the process provided by the invention, and are not described again in order to reduce repetition. Correspondingly, the technical details mentioned in the embodiment of the high-salinity high-organic wastewater zero-discharge treatment system provided by the invention can also be applied to the embodiment of the high-salinity high-organic wastewater zero-discharge treatment process.
The above is only a preferred embodiment of the present invention, and it is not intended to limit the scope of the invention, and various modifications and changes will occur to those skilled in the art. Any modification, equivalent replacement, improvement and the like made within the spirit and principle of the present invention shall be included in the scope of the present invention.
Claims (10)
1. A high-salt high-organic matter wastewater zero-discharge treatment process is characterized by comprising the following steps:
step S210: preheating high-salt high-organic wastewater by a first steam condenser and a preheater in sequence, enabling a first mixed solution formed by mixing the preheated high-salt high-organic wastewater with a circulating liquid of a first effect heater to enter the first effect heater, performing heat exchange with raw steam in the first effect heater to reach a preset temperature, condensing the raw steam to generate condensed water for recycling, and performing steam-liquid separation on the first mixed solution at the preset temperature in a first effect separator to generate secondary steam;
step S220: the secondary steam generated by the first effect separator enters a second effect heater, the wastewater evaporated and concentrated by the first effect separator enters the second effect heater, a second mixed solution formed by mixing the wastewater with a circulating liquid of the second effect heater is heated to a preset temperature by the secondary steam generated by the first effect separator, the secondary steam after heat exchange is condensed to generate condensed water for recycling, and the second mixed solution at the preset temperature is subjected to vapor-liquid separation in the second effect separator to generate secondary steam again;
step S230: the secondary steam generated by the second effect separator enters a third effect heater, the wastewater evaporated and concentrated by the second effect separator enters the third effect heater, a third mixed solution formed by mixing the wastewater with the circulating liquid of the third effect heater is heated to a preset temperature by the secondary steam generated by the second effect separator, the secondary steam after heat exchange is condensed to generate condensed water for recycling, and the third mixed solution at the preset temperature is subjected to vapor-liquid separation in the third effect separator to generate secondary steam again;
step S240: the secondary steam generated by the third effect separator enters the first steam condenser for condensation to form steam condensate water for recycling, the waste water evaporated and concentrated by the third effect separator generates crystallized salt in the third effect separator, a part of crystallized salt solution is subjected to solid-liquid separation by a crystallized salt separation device, the separated crystallized salt is dried and stored, a part of separated crystallized salt mother liquor returns to the third effect separator, the other part of separated crystallized salt mother liquor enters an externally-discharged mother liquor evaporator, the generated secondary steam enters the second steam condenser for condensation to form steam condensate water for recycling, the produced miscellaneous salt crystal solution passes through the externally-discharged mother liquor evaporator and is subjected to solid-liquid separation, miscellaneous salt solids obtained by solid-liquid separation are stored, and the miscellaneous salt mother liquor returns to a mother liquor storage tank.
2. The high-salinity high-organic matter wastewater zero-discharge treatment process as claimed in claim 1, further comprising the steps of:
step S250: the non-condensable gas in the first effect heater, the second effect heater and the third effect heater enters a vacuum device for vacuum pumping.
3. The high-salinity high-organic matter wastewater zero-discharge treatment process as claimed in claim 1, further comprising the steps of:
step S260: and non-condensable gas in the first steam condenser and the second steam condenser enters a vacuum device for vacuum pumping.
4. The high-salinity high-organic-matter wastewater zero-discharge treatment process of claim 1, wherein the step of recycling condensed water generated by condensing secondary steam after heat exchange in the step S220 specifically comprises:
and the secondary steam after heat exchange is condensed and enters a secondary steam condensation water tank through a secondary effect buffer tank.
5. The high-salinity high-organic wastewater zero-discharge treatment process according to claim 4, wherein the noncondensable gas in the secondary effect buffer tank and the secondary steam condensate tank enters a vacuum device for vacuum pumping.
6. The high-salinity high-organic-matter wastewater zero-discharge treatment process of claim 1, wherein the step of recycling condensed water generated by condensing secondary steam after heat exchange in the step S230 specifically comprises:
and the secondary steam after heat exchange is condensed and enters a secondary steam condensate water tank through a third effect buffer tank.
7. The high-salinity high-organic wastewater zero-discharge treatment process according to claim 6, wherein the noncondensable gas in the third-effect buffer tank and the secondary steam condensate tank enters a vacuum device for vacuum pumping.
8. The high-salinity high-organic wastewater zero-discharge treatment process of claim 1, wherein the circulating liquid between the first-effect heater and the first-effect separator is operated in a forced circulation mode; and/or the presence of a gas in the gas,
circulating liquid between the second-effect heater and the second-effect separator operates in a forced circulation mode; and/or the presence of a gas in the gas,
and circulating liquid between the third-effect heater and the third-effect separator operates in a forced circulation mode.
9. The high-salinity high-organic matter wastewater zero-discharge treatment process of claim 8, wherein a first-effect circulating pump is connected between the first-effect heater and the first-effect separator; a second-effect circulating pump is connected between the second-effect heater and the second-effect separator; and a third-effect circulating pump is connected between the third-effect heater and the third-effect separator.
10. The high-salinity high-organic wastewater zero-discharge treatment process of claim 1, wherein the types of the first effect heater, the second effect heater and the third effect heater are the same; and/or the presence of a gas in the gas,
the first effect separator, the second effect separator and the third effect separator are of the same type.
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